Classifications

• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
  • B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
  • B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
  • B01J23/24—Chromium, molybdenum or tungsten
  • B01J23/31—Chromium, molybdenum or tungsten combined with bismuth
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
  • B01J27/14—Phosphorus; Compounds thereof
  • B01J27/186—Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
  • B01J27/188—Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium with chromium, molybdenum, tungsten or polonium
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
  • B01J27/14—Phosphorus; Compounds thereof
  • B01J27/186—Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
  • B01J27/188—Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium with chromium, molybdenum, tungsten or polonium
  • B01J27/19—Molybdenum
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C253/00—Preparation of carboxylic acid nitriles
  • C07C253/24—Preparation of carboxylic acid nitriles by ammoxidation of hydrocarbons or substituted hydrocarbons
  • C07C253/26—Preparation of carboxylic acid nitriles by ammoxidation of hydrocarbons or substituted hydrocarbons containing carbon-to-carbon multiple bonds, e.g. unsaturated aldehydes
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
  • Y02P20/00—Technologies relating to chemical industry
  • Y02P20/50—Improvements relating to the production of bulk chemicals
  • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Definitions

• This invention relates; to the manufacture ofi' acr.ylo nitr-ile. It is: particularly concerned; the production of acryloilitl'ilefr'om propylene;
• H O-PR'oPYLENE RATIO A particularly surprising aspect of this invention isthe effect of water on. the course of the. reaction. I have found thatthepresence of water in. the mixture fedto the. reaction vessel improves the selectivity and yield of the reaction. so: far as. the productionof the acrylonitrile is; concerned Improvements on the order of several hundredpercenthave. been observed in the presence of Water as compared to similar runs made in the absence of added water. Consequently, the presence of water has a marked beneficial effect on this reaction, but reactions notincluding 'walter in the feed are not to be excluded from this invention. a
• the molar ratio of water to propylene'shtruld be at-least about 0 .2511. Ratiosnon the order of 1:1 are particularly desirable but higher ratios. may be employed, -i-:e.-, up toabout 10:1; Because of the recovery problems involved; it is generally preferred "to use only so much water as is. necessary to obtain the desired. improvement int'yield. Itis who understood that water does not bebe employedas the source of oxygen. From a purely technical viewpoint, relatively molecular oxygen will rvsequivaiear results. rheaneia'rmtio or oxygen to the olefin in the feed to the reaction vessel-shouldbe in the range of 0.5 :1 to 3:1 and aratio ar-about l':1' to 2:1 is preferred,
• thesaforementioned catalysts can be used alone or supported on carrier ma terials.
• Any suitable carrier material may be used, such as, for example,v silica.
• the catalyst may belprepared by any of the numerous methods of catalyst preparation which are known to those skilled in the art.
• the cat-alyst may be manufactured by co-gelling the various ingredients. The co-gelled mass may then be dried and ground to an appropriate size. Alternately, the co-gelled material may be slurried and spray dried in accordance with conventional techniques.
• the catalyst may be extruded as pellets or formed into spheres in oil as is well known in the art. Alternatively, the catalyst components may be mixed with the support in the form of the slurry followed by drying, or may be impregnated on silica or other support.
• the surface area of the catalyst is of some importance as I have found that high surface area catalysts tend to favor the further oxidation of the olefin to undesirable products. In general, the surface area of the catalyst should not exceed 750 sq. meters/ gram, but it does not appear that there is any lower limit on surface area. In some instances it may be desirable to heat treat the catalyst after preparation for the purpose of modifying the surface area and/or for the purpose of driving off those volatile ingredients which are included in the catalyst during the separation but which are necessary to its operability.
• the catalyst may be prepared in any convenient form as, for example, pellets or small particles suitable for use in a so-called fluidized reactor bed.
• the temperature at which the reaction is carried out may be any temperature in the range of 550 to 1000 F.
• the preferred temperature range runs from about 800 to 950 F.
• the pressure at which the reaction is conducted is also an important variable, and the reaction should be carried out at about atmospheric or slightly above atmospheric (2 to 3 atmospheres) pressure.
• high pressures -i.e., above 250 p.s.i.g., are not suitable for the process since higher pressures tend to favor the formation of undesirable by-products.
• the apparent contact time employed in the process is not especially critical, and contact times in the range of 0.1 to 50 seconds may be employed.
• the apparent contact time may be defined as the length of time in seconds which a unit volume of gas measured under the conditions of reaction is in contact with the apparent unit volume of the catalyst. It may be calculated, for example, from the apparent volume of the catalyst bed, the average temperature of the reactor, and the flow rates in the vessel of the components of the reaction mixture.
• the optimum contact time will, of course, vary depending upon the olefin being treated, but in general it may be said that a contact time of 1 to 15 seconds is preferred.
• any apparatus of the type suitable for carrying out oxidation reaction in the vapor phase may be employed in the execution of this process.
• the process may be conducted either continuously or intermittently.
• the catalyst bed may be a fixed bed employing a pelleted catalyst or, in the alternative, a so-called fluidized bed of catalyst may be employed.
• the fluidized bed offers definite advantages with regard to process control in that such a bed permits closer control of the temperature of the reaction as is well known to those skilled in the art.
• the reactor may be brought to the reaction temperature before or after the introduction of the reaction feed mixture. However, on a large scale operation it is preferred to carry out the process in a continuous manner, and in such a system the recirculation of the unreacted olefin is contemplated. Periodic regeneration or reactivation of the catalyst is also contemplated, and this may be accomplished, for example, by contacting the catalyst with air at an elevated temperature.
• the products of the reaction may be recovered by any of the methods known to those skilled in the art.
• One such method involves scrubbing the efiiuent gases from the reactor with cold water or an appropriate solvent to remove the products of the reaction.
• the ultimate recovery of the products may be accomplished by conventional means.
• the efiiciency of the scrubbing operation may be improved when water is employed as the scrubbing agent by adding a suitable wetting agent to the water.
• molecular oxygen is employed as the oxidizing agent in this process, the resulting product mixture remaining after the removal of the nitriles may be treated to remove carbon dioxide with the remainder of the mixture containing the unreacted propylene and oxygen being recycled through the reactor.
• the residual product after separation of the nitriles and other carbonyl products may be scrubbed with a non-polar solvent, e.g., a hydrocarbon fraction in order to recover unreacted propylene and in this case the remaining gases may be discarded.
• a non-polar solvent e.g., a hydrocarbon fraction
• a suitable inhibitor to prevent polymerization of the unsaturated products during the recovery steps is also contemplated.
• Example 18 A tin phosphomolybdate catalyst was prepared in the following manner:
• the yield of useful products on a carbon basis was 46.5%.
• Example 19 A bismuth phosphotungstate catalyst was prepared in the following manner:
• a process for the manufacture of acrylonitrile comprising the step of contacting in the vapor phase a mixture of propylene, ammonia and oxygen with a catalyst selected frornthe group consisting of the bismuth, tin, and antimony salts of phosphomolybdic and molybdic acids and bismuth phosphotungstate.
• a process for the manufacture of acrylonitrile which comprises the step of contacting in the vapor phase at a temperature of about 850 'F. a mixture of propylene, ammonia, and oxygen with a fluidized bed of catalyst'consisting essentially of bismuth phosphomolybdate' sup? ported on silica, said mixture having a molar ratio of propylene to ammonia of about 1:1 and a molar ratio of propylene to oxygen of about 1:2.

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• Chemical & Material Sciences (AREA)
• Organic Chemistry (AREA)
• Engineering & Computer Science (AREA)
• Materials Engineering (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
• Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
• Catalysts (AREA)

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• 0
  • MX MX67287D patent/MX67287A/es unknown
  • IT IT605134D patent/IT605134A/it unknown
  • CA CA718025A patent/CA718025A/en not_active Expired
  • MX MX64564D patent/MX64564A/es unknown
  • CA CA687664A patent/CA687664A/en not_active Expired
  • IT IT801567D patent/IT801567A/it unknown
• 1957
  • 1957-09-20 US US685352A patent/US2904580A/en not_active Expired - Lifetime
• 1958
  • 1958-08-18 GB GB26495/58A patent/GB867438A/en not_active Expired
  • 1958-09-11 FR FR774289A patent/FR1222460A/fr not_active Expired
  • 1958-09-12 NL NL231326A patent/NL107721C/xx active
  • 1958-09-13 DE DEST14237A patent/DE1127351B/de active Pending
  • 1958-09-13 BE BE571200D patent/BE571200A/xx unknown
• 1959
  • 1959-02-24 US US794841A patent/US3050546A/en not_active Expired - Lifetime
  • 1959-03-05 CH CH7038959A patent/CH385192A/fr unknown
• 1960
  • 1960-01-29 GB GB3303/60A patent/GB884437A/en not_active Expired
  • 1960-02-20 DK DK65260AA patent/DK102906C/da active
  • 1960-02-22 FR FR819209A patent/FR77200E/fr not_active Expired
  • 1960-02-22 BE BE587897D patent/BE587897A/xx unknown
  • 1960-02-23 DE DEST16146A patent/DE1180739B/de active Pending
  • 1960-02-24 NL NL248761A patent/NL110666C/xx active
  • 1960-02-24 CH CH209160A patent/CH404640A/fr unknown
• 1962
  • 1962-12-31 MY MY196220A patent/MY6200020A/xx unknown
• 1963
  • 1963-05-09 NL NL292532A patent/NL120493C/xx active

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